Composition that includes cyclohexyl-substituted tertiary alkanols

ABSTRACT

The present invention relates to processes for the preparation of compounds of the formula (Ia) 
                         
by reacting styrene with a secondary alkanol and the hydrogenation of the resulting phenyl-substituted tertiary alkanol. In addition, the invention relates to compounds of the formula (Ia) and to the use of such compounds as fragrances, and also to compositions which comprise compounds of the formulae (Ia) and (Ib).

CROSS-REFERENCE TO RELATED APPLICATIONS

This continuation application claims benefit under 35 U.S.C. §120 ofcopending U.S. application Ser. No. 14/090,626 filed Nov. 26, 2013,which in turn claims benefit under 35 U.S.C. §119(e) of U.S. ProvisionalApplication 61/730,104, filed Nov. 27, 2012, each application of whichis incorporated by reference in its entirety.

The present invention relates to a process for the preparation ofcyclohexyl-substituted tertiary alkanols, and to the use of suchcompounds as fragrance.

BACKGROUND OF THE INVENTION

Fragrances are used in a large number of technical products andhousehold products for concealing undesired intrinsic odors or forolfactory improvement. Floral notes are of great interest here,especially for use in detergents and cleaners. It is important for usesof this type that the fragrances not only have a pleasant odor but alsoremain chemically stable even over a prolonged period and can beincorporated in a technically easy manner into the correspondingproduct. The availability of as cost-effective as possible a productionprocess for the fragrances is also desirable.

4-Cyclohexyl-2-methyl-2-butanol, which is also referred to as coranol,is a fragrance with a lily of the valley scent, the use of which as aconstituent of scent compositions was described for the first time inU.S. Pat. No. 4,701,278. Preparation processes for4-cyclo-hexyl-2-methyl-2-butanol have been described by Okazawa et al.(Can. J. Chem. 60 (1982), 2180-93) and Ebel et al. (WO 2011/117360).

DETAILED DESCRIPTION OF THE INVENTION

In principle, there is a continuing need for new fragrances tosupplement the existing pallet of fragrances. In searching for newfragrances which meet the aforementioned requirements, it has nowsurprisingly been found that cyclohexyl-substituted tertiary alkanolssuch as 1-cyclohexyl-3-methyl-3-pentanol and its relatively long-chainanalogs have interesting olfactory properties. As well as a pleasantlavender note (similar to coranol, tetrahydrolinalool),1-cyclohexyl-3-methyl-3-pentanol, for example, additionally has fruityaspects.

Furthermore, a new process for the preparation of such compounds hasbeen found. Synthesis routes for obtaining1-cyclohexyl-3-methyl-3-pentanol are described by Dazlauskas (Chemiya,Technika, Fizine Geografiya (4): 35-42, 1967) and also Nazarov andNagibina (Izvestiya Akademii Nauk SSSR, Seriya Khimicheskaya: 83-89,1946). However, these production pathways involve many stages and wouldconsequently be associated with high costs in the event of practicalconversion to an industrial scale.

The present invention provides a process for the preparation of acompound of the formula (Ia)

comprising:

a) the reaction of styrene with a compound of the formula (II)

giving a compound of the formula (IIIa)

and

b) the heterogeneous-catalytic hydrogenation of the compound of theformula (IIIa) to give the compound of the formula (Ia).

Unless stated otherwise, in the compounds of the formulae (Ia), (Ib),(II), (IIIa), (IIIb), (IV) and (V) described here and below, R¹ and R²,independently of one another, are selected from groups of the formula(C₃₋₇-cycloalkyl)_(x)-(C₁₋₇-alkyl)_(y), wherein either each of x and yis 1, or one of the variables x and y is 1 and the other is 0.Preferably, R¹ and R², independently of one another, are selected fromC₁₋₇alkyl, C₃₋₇-cycloalkyl and C₄₋₇-cycloalkylalkyl. Here, R¹ and R²together comprise in total 3 to 11 carbon atoms, in particular 3 to 8carbon atoms, preferably 3 to 5 carbon atoms and particularly preferably3 carbon atoms.

As used here, C₁₋₇-alkyl is a linear or branched alkyl radical having 1to 7 carbon atoms. Examples of linear C₁₋₇-alkyl are methyl, ethyl,n-propyl, n-butyl, n-pentyl and n-hexyl. Examples of branched C₁₋₇-alkylare isopropyl, sec-butyl, tert-butyl, isohexyl, 1-methylpentyl,2-methylpentyl, 3-methylpentyl, 1,1-dimethylbutyl, 2,2-dimethylbutyl,3,3-dimethylbutyl and 2-ethylbutyl.

As used here, C₃₋₇-cycloalkyl is a cycloalkyl radical having in total 3to 7 carbon atoms which is bonded via one of the carbon ring atoms. Thiscycloalkyl radical is not substituted or is substituted with 1, 2 or 3C₁₋₇-alkyl radicals, as defined above, with the proviso that thecycloalkyl radical comprises in total (i.e. including any alkylsubstituents) not more than 7 carbon atoms. Examples of an unsubstitutedC₃₋₇-cycloalkyl are cyclopropyl, cyclobutyl, cyclopentyl and cyclohexyl.

As used here, C₄₋₇-cycloalkylalkyl is a cycloalkyl group-substitutedlinear or branched alkyl radical which comprises in total (i.e.including the cycloalkyl substituent) 4 to 7 carbon atoms. Examples ofC₄₋₇-cycloalkylalkyl are cyclohexylmethyl, cyclopentylmethyl and1-cyclopentylethyl.

According to one preferred aspect of the invention, R¹ and R²,independently of one another, are selected from C₁₋₇-alkyl andC₃₋₇-cycloalkyl. The respective compounds within one specific reactionroute of the described reaction routes (also referred to below as“corresponding compounds”) carry the same R¹ and R².

A preferred embodiment of the invention relates to a process for thepreparation of 1-cyclohexyl-3-methyl-3-pentanol, comprising:

a) the reaction of styrene with 2-butanol, giving3-methyl-1-phenyl-3-pentanol, and

b) the heterogeneous-catalytic hydrogenation of3-methyl-1-phenyl-3-pentanol to give 1-cyclohexyl-3-methyl-3-pentanol.

In further embodiments of the process according to the invention, thecompound of the formula (Ia) is selected from1-cyclohexyl-3-methyl-3-hexanol, 1-cyclohexyl-3-methyl-3-heptanol,1-cyclohexyl-3-methyl-3-octanol, 1-cyclohexyl-3-methyl-3-nonanol,1-cyclohexyl-3,4-dimethyl-3-octanol,1-cyclohexyl-3,5-dimethyl-3-octanol,1-cyclohexyl-3,6-di-methyl-3-octanol,1-cyclohexyl-3,7-dimethyl-3-octanol,1-cyclohexyl-3,4,4-trimethyl-3-heptanol,1-cyclohexyl-3,5,5-trimethyl-3-heptanol,1-cyclohexyl-3,6,6-trimethyl-3-heptanol.1-cyclohexyl-5-ethyl-3-methyl-3-heptanol,1-cyclohexyl-3,5-dimethyl-3-heptanol,2,4-dicyclohexyl-2-methyl-2-butanol,1-cyclohexyl-4-cyclopentyl-3-methyl-3-pentanol,1-cyclohexyl-3-ethyl-3-hexanol, 1-cyclohexyl-3-ethyl-3-heptanol,1-cyclohexyl-3-ethyl-3-octanol and 1-cyclohexyl-3-ethyl-3-nonanol.

The process for the preparation of the compound of the formula (Ia) canbe depicted by the following reaction scheme:

The invention thus relates to a process for the preparation of acompound of the formula (Ia) with the steps described here and below andalso in the claims.

The process is associated with a number of advantages. It permits anextremely high atom-economic preparation of a compound of the formula(Ia) from very inexpensive basic chemicals, manages without complexwork-up steps and is consequently comparatively cost-effective. The useof expensive and hazardous reagents such as methyllithium is notrequired.

Both step a) and step b) can be carried out without problems on anindustrial scale and produce the respective products with highselectivity and good yields. In step a) of the process according to theinvention, a secondary alkanol of the formula (II) is reacted withstyrene. Here, in the sense of a hydroxyalkylation, a correspondingphenyl-substituted tertiary alkanol of the formula (IIIa) is formed, andalso, as by-products, inter alia toluene and ethylbenzene, althoughthese can be separated off from the target product for example bydistillation.

Furthermore, in step a), besides the compound of the formula (IIIa), thecorresponding (i.e. identical R¹, R²) methyl-substituted alkanol of theformula (IIIb)

can be formed, from which, as a result of heterogeneous-catalytichydrogenation, the compound of the formula (Ib)

arises.

The methyl-substituted alkanol of the formula (IIIb) arises presumablyas a result of the reaction of the compound of the formula (II) withα-methylstyrene, which can be formed in a radical reaction according tothe following scheme from styrene and ethylbenzene:

With regard to the selectivity of the reaction, it has proven to beadvantageous if the reaction in step a) is carried out undersupercritical conditions. These are understood as meaning reactionconditions under which at least one of the components of the reactionmixture, preferably the compound of the formula (II), is present in thesupercritical state. Accordingly, according to a preferred embodiment ofthe process according to the invention, the reaction in step a) takesplace under conditions under which the compound of the formula (II) ispresent in the supercritical state. In the case of 2-butanol, forexample, the critical temperature T_(c) is 263° C. and the criticalpressure P_(c) is 4.2 MPa. Supercritical conditions can be adjusted bythe person skilled in the art by varying the pressure and temperature.

The temperature required for an adequate rate of the reaction of styrenewith a compound of the formula (II) is generally at least (T_(c)+15)°C., often at least (T_(c)+65)° C. and in particular at least (T_(c)+85)°C., where T_(c) is the critical temperature of the compound of theformula (II) used. To achieve an adequate selectivity of the reaction,it has proven to be advantageous if the temperature during the reactionin step a) does not exceed a value of (T_(c)+265)° C., in particular(T_(c)+165)° C. The reaction in step a) preferably takes place atincreased pressure, which is generally in the range from 5 to 50 MPa,often in the range from 10 to 30 MPa and in particular in the range from15 to 25 MPa. Preferably, the reaction takes place under the intrinsicpressure of the reaction mixture prevailing at the desired reactiontemperature.

The reaction time naturally depends on the selected conditions and thedesired conversion and is usually in the range from 30 s to 4 h, inparticular in the range from 3 min to 3 h and specifically in the rangefrom 5 min to 2.5 h. In one embodiment of the invention, the reactiontime is in the range from 0.5 to 4 h, in particular in the range from 1to 3 h and specifically in the range from 1.5 to 2.5 h. As a rule, thereaction is carried out until the reactant used in deficit, which ispreferably styrene, has been reacted to at least 80%, in particular toat least 90%.

It has proven to be particularly advantageous to carry out the reactionin step a) at elevated temperatures, i.e. above (T_(c)+65)° C., inparticular above (T_(c)+85)° C., preferably in the range (T_(c)+115)° C.and (T_(c)+165)° C. This allows short reaction times which are usuallyin the range from 30 s to 30 min, in particular in the range from 3 minto 20 min and specifically in the range from 5 min to 15 min. In thisway, good selectivities as regards the target product can also beachieved for a high conversion of styrene.

With regard to the selectivity of the reaction, it has proven to beadvantageous if the reaction in step a) is carried out in the extensiveor complete absence of catalysts, such as, for example, radicalstarters, acids or transition metal compounds. Extensive absence meansthat the concentration of any catalysts is less than 1 g/kg (<1000 ppm),in particular less than 0.1 g/kg (<100 ppm), based on the total weightof the reaction mixture.

The reaction of styrene with a compound of the formula (II) in step a)can be carried out without dilution or in a diluent that is suitable,i.e. inert under reaction conditions. Suitable inert diluents areaprotic organic solvents which have no ethylenically unsaturated doublebond, such as, for example, aliphatic and alicyclic ethers havingpreferably 4, 5 or 6 carbon atoms, e.g. diethyl ether,1,2-dimethmwethane, bis(2-methoxyethyl) ether, 2-methyltetrahydrofuranand in particular tetrahydrofuran; aliphatic and cycloaliphaticsaturated hydrocarbons having preferably 5 to 8 carbon atoms, e.g.pentane, hexane, heptane or octane; alkyl esters of aliphatic carboxylicacids having preferably 4 to 8 carbon atoms and mixtures of theaforementioned solvents. Preferably, the reaction in step a) takes placewithout dilution, i.e. essentially no feed materials different fromstyrene and the compound of the formula (II), such as, for example,inert solvents, are used for the reaction. Essentially here means thatstyrene and the compound of the formula (II) constitute at least 95% byweight, in particular at least 99% by weight, based on the total amountof the components used in step a). In addition, the reactants used forthe reaction, i.e. styrene and the compound of the formula (II), maycomprise, as a result of manufacture, small amounts of impurities suchas water, ethylbenzene, toluene and the like, the contaminants generallyconstituting less than 5% by weight, in particular less than 1% byweight, based on the total amount of the reactants. In particular, thewater content of the reactants used in step a) is not more than 1% byweight, based on the total amount of the reactants.

As regards the selectivity of the reaction, it has proven to beadvantageous if, in the reaction according to step a), a compound of theformula (II) is used in large excess, based on styrene, and/or it isensured that, in the reaction zone in which styrene and the compound ofthe formula (II) are brought into contact with one another underreaction conditions, there is a high excess of the compound of theformula (II), based on the styrene located in the reaction zone. As arule, in step a), styrene and the compound of the formula (II) arereacted in a molar ratio of styrene to compound of the formula (II) ofat most 1:5, preferably at most 1:10, in particular at most 1:30,particularly preferably at most 1:40 and specifically at most 1:50. Withregard to an efficient reaction procedure, it is advantageous if, instep a), styrene and compound of the formula (II) are used in a molarratio in the range from 1:5 to 1:200, preferably in the range from 1:10to 1:200, in particular in the range from 1:30 to 1:150 or in the rangefrom 1:30 to 1:130, particularly preferably in the range from 1:40 to1:100 and specifically in the range from 1:50 to 1:90.

The reaction in step a) can be carried out batchwise (so-called batchmode), i.e. the styrene and the compound of the formula (II) areintroduced as initial charge in the desired molar ratio in a suitablereactor and brought to the desired reaction conditions and held underreaction conditions until the desired conversion is attained. Thereaction in step a) can also be carried out in the so-called semi-batchmode, i.e. the majority, as a rule at least 80%, in particular at least90%, of one or both reactants, is added to the reactor under reactionconditions continuously or in portions over an extended period,generally at least 50% of the total reaction time. For example, at least80%, in particular at least 90%, of the compound of the formula (II)used, optionally together with some of the styrene, can be introduced asinitial charge, and at least 80%, in particular at least 90%, of thestyrene used can be supplied to the reaction under reaction conditions.

The reaction in step a) can also be carried out continuously, i.e.styrene and compound of the formula (II) are fed continuously into areaction zone in the desired molar ratio and the reaction mixture isremoved continuously from the reaction zone. The rate at which styreneand compound of the formula (II) are supplied to the reaction zone isgoverned by the desired residence time, which for its part depends in aknown manner on the reactor geometry and corresponds to the reactiontime stated above.

The reaction in step a) can in principle be carried out in all reactorswhich are suitable for the selected reaction conditions, preferably inautoclaves, which can have devices for mixing the reactants, or inreaction tubes.

In order to keep the molar ratio of styrene to compound of the formula(II) low during the reaction and at the same time to permit an efficientreaction procedure, it has proven to be advantageous if at least 80%, inparticular at least 90%, of the compound of the formula (II) used instep a), optionally together with some of the styrene, is introduced asinitial charge, and at least 80%, in particular at least 90%, of thestyrene used in step a) is supplied to the reaction in step a) underreaction conditions. The addition of the styrene can take place inportions or preferably continuously. The rate at which styrene issupplied here is preferably selected such that the molar ratio of thestill unreacted styrene fed into the reaction zone or the reactor to thecompound of the formula (II) located in the reaction zone during thereaction is less than 1:10, in particular not more than 1:40 andspecifically not more than 1:50 and is e.g. in the range from 1:10 to1:2000, preferably in the range from 1:40 to 1:1500 and in particular inthe range from 1:50 to 1:1000. In the case of a continuous reactionprocedure, styrene and compound of the formula (II) will therefore besupplied to the reactor or the reaction zone in the aforementioned molarratios. In a specific embodiment of the invention, the rate at whichstyrene is supplied is preferably selected such that the molar ratio ofthe styrene fed into the reaction zone or the reactor to the compound ofthe formula (II) located in the reaction zone is in the range from 1:10to 1:130, in particular in the range from 1:20 to 1:120, particularlypreferably in the range from 1:40 to 1:100 and specifically in the rangefrom 1:50 to 1:90. This is the case in particular also for a continuousreaction procedure for the molar ratios of styrene and compound of theformula (II) supplied to the reactor or the reaction zone.

The reaction mixture obtained in step a) can be worked up in a mannerknown per se or, optionally after removing the compound of the formula(II), be used directly as such in step b) of the process according tothe invention. As a rule, it has proven to be advantageous to work upthe reaction mixture produced in step a), for example extractively ordistillatively or by a combination of these measures. In one embodimentof the process according to the invention, the reaction mixture producedin step a) is worked up distillatively, in which case the desiredcompound of the formula (IIIa) or the desired composition consistingessentially of the compound of the formula (IIIa) and the correspondingcompound of the formula (IIIb) is separated off as middle fraction fromlow boilers and high boilers. If an excess of compound of the formula(II) is used in the process, the low boiling fraction, which consistspredominantly of compound of the formula (II), can be returned to theprocess. As a rule, prior to step b), the compound of the formula (II)will be largely removed, such that the fraction of compound of theformula (II) in the starting material used for the hydrogenation in stepb) is less than 20% by weight, in particular not more than 10% byweight, based on the total amount of starting material in step b).

Depending on the configuration of the distillation, the essentially purecompound of the formula (IIIa) (purity at least 95% by weight, inparticular at least 98% by weight and specifically at least 99% byweight or at least 99.5% by weight) or a composition which consistsessentially, i.e. to at least 95% by weight, in particular at least 98%by weight and specifically at least 99% by weight or at least 99.5% byweight, of compound of the formula (IIIa) and corresponding compound ofthe formula (IIIb), where the molar ratio of the compound of the formula(IIIa) to the corresponding compound of the formula (IIIb) is typicallyin the range from 50:1 to 1000:1 is/are obtained.

Both the pure compound of the formula (IIIa) and also the compositioncan be used in the subsequent hydrogenation according to step b). Thisgives rise to the corresponding pure compound of the formula (Ia)(purity at least 95% by weight, in particular at least 98% by weight andspecifically at least 99% by weight or at least 99.5% by weight) or thecorresponding composition of compound of the formula (Ia) and compoundof the formula (Ib) (purity and weight ratio of the compounds of theformulae (Ia) and (Ib) essentially as defined above for the compounds ofthe formulae (IIIa) and (IIIb)).

The hydrogenation expediently takes place over a catalyst suitable forthe ring hydrogenation of aromatics, which is also referred to belowsimply as catalyst. Suitable catalysts are in principle all catalystswhich are known to be suitable for the ring hydrogenation of aromatics,i.e. catalysts which catalyze the hydrogenation of phenyl groups tocyclohexyl groups. These are usually catalysts which comprise at leastone active metal from group VIIIB of the Periodic Tables (CAS version),such as e.g. palladium, platinum, cobalt, nickel, rhodium, iridium,ruthenium, in particular ruthenium, rhodium or nickel, or comprise amixture of two or more thereof, optionally in combination with one ormore further active metals. Preferred further active metals are selectedfrom groups IB or VIIB of the Periodic Tables (CAS version). Among themetals of subgroups IB and/or VIIB that can likewise be used, e.g.copper and/or ruthenium are suitable.

The catalysts can be unsupported catalysts or, preferably, supportedcatalysts. Suitable support materials are, for example, activatedcarbon, silicon carbide, silicon dioxide, aluminum oxide, magnesiumoxide, titanium dioxide, zirconium dioxide, aluminosilicates andmixtures of these support materials. The amount of active metal isusually 0.05 to 10% by weight, often 0.1 to 7% by weight and inparticular 0.1 to 5% by weight, based on the total weight of thesupported catalyst, particularly if the active metal is a precious metalsuch as rhodium, ruthenium, platinum, palladium or iridium. In catalystswhich comprise cobalt and/or nickel as active metals, the amount ofactive metal can be up to 100% by weight and is usually in the rangeform 1 to 100% by weight, in particular 10 to 90% by weight, based onthe total weight of the catalyst.

The supported catalysts can be used in the form of a powder. As a rule,such a powder has particle sizes in the range from 1 to 200 μm, inparticular 1 to 100 μm. Pulverulent catalysts are suitable particularlywhen the catalyst is suspended in the reaction mixture to behydrogenated (suspension mode). When using the catalysts in catalystfixed beds, moldings are usually used; these are obtainable e.g. byextrusion or tableting and can have e.g. the shape of spheres, tablets,cylinders, strands, rings or hollow cylinders, stars and the like. Thedimensions of these moldings usually fluctuate in the range from 0.5 mmto 25 mm. Catalyst strands with strand diameters of from 1.0 to 5 mm andstrand lengths of from 2 to 25 mm are often used. Higher activities cangenerally be achieved with smaller strands, but these often do notexhibit adequate mechanical stability in the hydrogenation process.Consequently, very particular preference is given to using strands withstrand diameters in the range from 1.5 to 3 mm. Preference is likewisegiven to spherical support materials with sphere diameters in the rangefrom 1 to 10 mm, in particular 2 to 6 mm.

Preferred catalysts are those which comprise at least one active metalselected from ruthenium, rhodium and nickel, optionally in combinationwith one or more further active metals which are selected from thegroups IB, VIIB and VIIIB of the Periodic Table (CAS version).

Particularly preferred catalysts are ruthenium-containing catalysts.These comprise ruthenium as active metal, optionally in combination withone or more further active metals. Preferred further active metals areselected from the groups IB, VIIB and VIIIB of the Periodic Table (CASversion). The catalysts may be unsupported catalysts or, preferably,supported catalysts. Examples of further active metals from the groupVIIIB are e.g. platinum, rhodium, palladium, iridium, cobalt and nickel,which can also be used as a mixture of two or more thereof. Among themetals of subgroups IB and/or VIIB that can likewise be used, copperand/or rhenium, for example; are suitable. Preference is given to usingruthenium, on its own as active metal or together with platinum oriridium as active metal; very particular preference is given to usingruthenium on its own as active metal.

Preference is given in particular to ruthenium-containing catalysts inwhich the ruthenium, and also the optionally present further activemetals, are arranged on a support material (ruthenium-containingsupported catalysts). Suitable support materials for theruthenium-containing supported catalysts are in principle theaforementioned support materials. Preference is given to silicondioxide-containing support materials, in particular those which have acontent of silicon dioxide of at least 90% by weight, based on the totalweight of the support material. Preference is likewise given to aluminumoxide-containing support materials, in particular those which have acontent of aluminum oxide (calculated as Al₂O₃) of at least 90% byweight, based on the total weight of the support material. Preferably,the support materials have a specific BET surface area, determined by N₂adsorption in accordance with DIN 66131, of at least 30 m²/g, inparticular 50 to 1000 m²/g. The amount of active metal is usually 0.05to 10% by weight, preferably 0.1 to 3% by weight and in particular 0.1to 1% by weight, based on the total weight of the ruthenium-containingsupported catalyst.

Suitable ruthenium-containing catalysts are, for example, the catalystsspecified in U.S. Pat. No. 3,027,398, DE 4407091, EP 258789, EP 813906,EP 1420012, WO 99/32427, WO 00/78704, WO 02/100536, WO 03/103830, WO2005/61105, WO 2005/61106, WO 2006/136541 and WO2011082991. As regardsthe catalysts disclosed therein, reference is made to these documents.

Likewise preferred catalysts are rhodium-containing catalysts. Thesecomprise rhodium as active metal, optionally in combination with one ormore further active metals. Preferred further active metals are selectedfrom the groups IB, VIIB or VIIIB of the Periodic Table (CAS version).The catalysts may be unsupported catalysts or preferably supportedcatalysts. Examples of further active metals from the group VIIIB aree.g. platinum, palladium, iridium, cobalt and nickel, which can also beused as a mixture of two or more thereof. Among the metals of subgroupsIB and/or VIIB that can likewise be used, copper and/or rhenium, forexample, are suitable. In these catalysts, rhodium is used on its own asactive metal or together with platinum or iridium as active metal; veryparticular preference is given to using rhodium on its own as activemetal. Suitable rhodium-containing catalysts are known for example fromthe publications specified above for rhenium-containing catalysts, canbe prepared by the procedures indicated therein or are commerciallyavailable, e.g. the catalyst Escat 34 from Engelhard. Forrhodium-containing supported catalysts, the aforementioned supportmaterials are in principle suitable. Preference is given to silicondioxide-containing support materials, in particular those which have acontent of silicon dioxide of at least 90% by weight, based on the totalweight of the support material. Preference is likewise given to aluminumoxide-containing support materials, in particular those which have acontent of aluminum oxide (calculated as Al₂O₃) of at least 90% byweight, based on the total weight of the support material. The amount ofactive metal is usually 0.05 to 10% by weight, based on the total weightof the rhodium-containing supported catalyst.

Likewise preferred catalysts are nickel-containing catalysts. Thesecomprise nickel as active metal, optionally in combination with one ormore further active metals. Preferred further active metals are selectedfrom the groups IB, VIIB or VIIIB of the Periodic Table (CAS version).The catalysts may be unsupported catalysts or preferably supportedcatalysts. Examples of further active metals from the group VIIIB aree.g. platinum, palladium, iridium and cobalt, which can also be used asa mixture of two or more thereof. Among the metals of subgroups IBand/or VIIB that can likewise be used, copper and/or rhenium, forexample, are suitable. In these catalysts, nickel is preferably used onits own as active metal. Suitable nickel-containing catalysts arecommercially available, for example the catalyst Ni5249P from BASF SE.For nickel-containing supported catalysts, the aforementioned supportmaterials are in principle suitable. Preference is given to silicondioxide-, aluminum oxide- and magnesium oxide-containing supportmaterials, in particular those which consist to at least 90% by weightof such materials. The amount of active metal is usually 1 to 90% byweight, preferably 10 to 80% by weight and in particular 30 to 70% byweight, based on the total weight of the nickel-containing supportedcatalyst. Preference is also given to those nickel-containing catalystswhich consist essentially exclusively of active metal, i.e. their amountof active metal is more than 90% by weight, e.g. 90 to 100% by weight.

According to one particularly preferred embodiment, a coated catalyst isused, in particular a coated catalyst which has, as active metal,ruthenium on its own or together with at least one further active metalof subgroups IB, VIIB or VIIIB of the Periodic Tables in theaforementioned amounts. Coated catalysts of this type are known inparticular from WO 2006/136541 and also in the previously unpublished EP09179201.0.

A coated catalyst of this type is a supported catalyst in which themajority of the active metal present in the catalyst is located in thevicinity of the surface of the catalyst. In particular, at least 60% byweight, particularly preferably at least 80% by weight, in each casebased on the total amount of the active metal, are present to apenetration depth of at most 200 μm, i.e. in a shell with a distance ofat most 200 μm from the surface of the catalyst particles. By contrast,only a very small amount, if any, of the active metal is present in theinterior (core) of the catalyst. In the process according to theinvention, very particular preference is given to using a shell catalystin which no active metal can be detected in the interior of thecatalyst, i.e. active metal is present only in the outermost shell, forexample in a zone down to a penetration depth of 100 to 200 μm. Theaforementioned data can be ascertained by means of SEM (scanningelectron microscopy), EPMA (electron probe microanalysis) EDXS (energydispersive X-ray spectroscopy) and are averaged values. Further data asregards the aforementioned measurement methods and techniques can befound for example in “Spectroscopy in Catalysis” by J. W.Niemantsverdriet, VCH, 1995. As regards further details concerning thepenetration depth of active metal, reference is made to WO 2006/136541,in particular to p. 7, lines 6 to 12.

Preferred coated catalysts have a content of active metal in the rangefrom 0.05 to 1% by weight, in particular 0.1 to 0.5% by weight,particularly preferably 0.25 to 0.35% by weight, in each case based onthe total weight of the catalyst.

For the hydrogenation according to the invention in step b), coatedcatalysts with a support material based on silicon dioxide, in generalamorphous silicon dioxide, are particularly preferred. In thisconnection, the term “amorphous” is understood as meaning that thefraction of crystalline silicon dioxide phases constitutes less than 10%by weight of the support material. The support materials used forproducing the catalysts can however have superstructures which areformed by regular arrangement of pores in the carrier material. Suitablesupport materials are in principle amorphous silicon dioxide gradeswhich consist at least to 90% by weight of silicon dioxide, in whichcase the remaining 10% by weight, preferably not more than 5% by weight,of the support material can also be a different oxidic material, e.g.,MgO, CaO, TiO₂, ZrO₂, Fe₂O₃ and/or alkali metal oxide. In a preferredembodiment of the coated catalyst, the support material is halogen-free,in particular chlorine-free, i.e. the content of halogen in the supportmaterial is less than 500 ppm by weight, e.g. in the range from 0 to 400ppm by weight. Consequently, preference is given to a coated catalystwhich comprises less than 0.05% by weight of halide (determined by ionchromatography), based on the total weight of the catalyst. Preferenceis given to support materials which have a specific surface area in therange from 30 to 700 m²/g, preferably 30 to 450 m²/g, (BET surface areain accordance with DIN 66131). Suitable amorphous support materialsbased on silicon dioxide are known to the person skilled in the art andare commercially available (see e.g. O. W. Flörke, “Silica” in Ullmann'sEncyclopedia of Industrial Chemistry, 6th Edition on CD-ROM). They canhave been produced either from natural origin or else synthetically.Examples of suitable amorphous support materials based on silicondioxide are silica gels, kieselguhr, pyrogenic silicas and precipitatedsilicas. In a preferred embodiment of the invention, the catalysts usedhave silica gels as support materials. Depending on the configuration ofthe coated catalyst, the support material can take various forms. If theprocess according to the invention in which the coated catalysts areused is designed as a suspension process, then the support material willusually be used in the form of a finely divided powder for producing thecatalysts used. Preferably, the powder has particle sizes in the rangefrom 1 to 200 μm in particular 1 to 100 μm. When using the coatedcatalyst according to the invention in catalyst fixed beds, moldings, asdescribed above, of the support material are usually used.

In a particularly preferred embodiment, the support material of thecoated catalyst used, which is in particular a support material based onsilicon dioxide, has a pore volume in the range from 0.6 to 1.0 ml/g,preferably in the range from 0.65 to 0.9 ml/g, for example from 0.7 to0.8 ml/g, determined by Hg porosimetry (DIN 66133), and a BET surfacearea in the range from 280 to 500 m²/g, preferably in the range from 280to 400 m²/g, very particularly preferably in the range from 300 to 350m²/g. Preferably, in coated catalysts of this type, at least 90% of thepores present have a diameter of from 6 to 12 nm, preferably 7 to 11 nm,particularly preferably 8 to 10 nm. The pore diameter can be determinedby means of methods known to the person skilled in the art, for exampleby Hg porosimetry or N₂-physisorption. In a preferred embodiment, atleast 95%, particularly preferably at least 98%, of the pores presenthave a pore diameter of from 6 to 12 nm, preferably 7 to 11 nm,particularly preferably 8 to 10 nm. In a preferred embodiment, no poreswhich are smaller than 5 nm are present in these coated catalysts.Furthermore, no pores larger than 25 nm, in particular larger than 15nm, are preferably present in these coated catalysts. In this connection“no pores” means that no pores with these diameters are found usingcustomary measurement methods, for example Hg porosimetry or N₂physisorption.

In preferred coated catalysts, the dispersity of the active metal ispreferably 30 to 60% and particularly preferably 30 to 50%. Methods formeasuring the dispersity of the active metal are known to the personskilled in the art and include, for example, pulse chemisorption, inwhich the determination of the precious metal dispersion (specific metalsurface area, crystallite size) is carried out with a CO pulse method(DIN 66136(1-3)).

The hydrogenation process according to the invention can be carried outin the liquid phase or in the gas phase. Preference is given to carryingout the hydrogenation process according to the invention in the liquidphase.

The hydrogenation process according to the invention can be carried outeither in the presence or the absence of a solvent or diluent, i.e. itis not absolutely necessary to carry out the hydrogenation in solution.Solvents or diluents which can be used are any suitable solvents ordiluents. Suitable solvents or diluents are in principle those which areable to dissolve the organic compound to be hydrogenated as completelyas possible or are completely miscible therewith and which are inert,i.e. are not hydrogenated, under the hydrogenation conditions. Examplesof suitable solvents are cyclic and acyclic ethers having preferably 4to 8 carbon atoms, e.g. tetrahydrofuran, dioxane, methyl tert-butylether, dimethoxyethane, dimethoxypropane, dimethyldiethylene glycol,aliphatic alcohols having preferably 1 to 6 carbon atoms such asmethanol, ethanol, n- or isopropanol, n-, 2-, iso- or tert-butanol,carboxylic acid esters of aliphatic carboxylic acids having preferably 3to 8 carbon atoms such as methyl acetate, ethyl acetate, propyl acetateor butyl acetate, methyl propionate, ethyl propionate, butyl propionate,and also aliphatic ether alcohols such as methoxy propanol andcycloaliphatic compounds such as cyclohexane, methylcyclohexane anddimethylcyclohexane. The amount of solvent or diluent used is notlimited in a particular manner and can be freely chosen as necessary,although when using a solvent preference is given to those amounts whichlead to a 3 to 70% strength by weight solution of the organic compoundprovided for the hydrogenation.

In one embodiment of the invention, the step b) according to theinvention is carried out without dilution.

The actual hydrogenation usually takes place analogously to the knownhydrogenation processes for the hydrogenation of organic compounds whichhave hydrogenable groups, preferably for the hydrogenation of acarbocyclic aromatic group to give the corresponding carbocyclicaliphatic groups, as described in the prior art cited at the start. Forthis, the organic compound is brought into contact, as the liquid phaseor gas phase, preferably as liquid phase, with the catalyst in thepresence of hydrogen. The liquid phase can be passed over a fluidizedcatalyst bed (fluidized bed mode) or a fixed catalyst bed (fixed bedmode).

The hydrogenation can be designed to be continuous or discontinuous,with the continuous procedure being preferred. Preferably, the processaccording to the invention is carried out in trickle reactors or inflooded mode by the fixed bed mode, the procedure in trickle reactorsbeing particularly preferred. In particular, the compound to behydrogenated is used without dilution, i.e. extensive absence of organicdiluents (solvent content preferably <10%). The hydrogen here can bepassed over the catalyst either cocurrently with the solution of thestarting material to be hydrogenated, or else countercurrently. Thehydrogenation can also be carried out discontinuously by the batch mode.In this case, the hydrogenation will preferably be carried out in anorganic solvent or diluent.

In the case of a discontinuous procedure of the process according to theinvention, in step b), the catalyst is typically used in an amount suchthat the concentration of ruthenium in the reaction mixture used for thehydrogenation is in the range from 10 to 10 000 ppm, in particular inthe range from 50 to 5000 ppm, specifically in the range form 100 to1000 ppm.

The hydrogenation typically takes place at a hydrogen pressure in therange from 5 to 50 MPa, in particular in the range from 10 to 30 MPa.The hydrogen can be fed into the reactor as it is, or diluted with aninert material, for example nitrogen or argon.

The hydrogenation in step b) typically takes place at temperatures above50° C., in particular in the range from 100 to 250° C.

Apparatuses suitable for carrying out the hydrogenation are known to theperson skilled in the art and are determined primarily by the mode ofoperation. Suitable apparatuses for carrying out a hydrogenationaccording to the hydrogenation on the fluidized catalyst bed and on thefixed catalyst bed are known e.g. from Ullmann's Encyclopedia ofIndustrial Chemisty, 4^(th) edition, volume 13, p. 135 ff., and alsofrom P. N. Rylander, “Hydrogenation and Dehydrogenation” in Ullmann'sEncyclopedia of Industrial Chemistry, 5^(th) edition on CD-ROM.

Compounds of the formula (Ia), where R¹ and R², independently of oneanother, are selected from groups of the formula(C₃₋₇-cycloalkyl)_(x)-(C₁₋₇-alkyl), wherein either each of x and y is 1,or one of the variables x and y is 1 and the other is 0, and R¹ and R²together comprise in total 4 to 11 carbon atoms, 5 to 11 carbon atoms,in particular 4 to 8 carbon atoms and preferably 4 or 5 carbon atoms,are likewise provided by the invention. If R¹ and R² together comprisein total 4 carbon atoms, each of R¹ and R² is preferably ethyl.Compounds of the formula (Ia) according to the invention can thus beselected for example from 1-cyclohexyl-3-methyl-3-heptanol,1-cyclohexyl-3-methyl-3-octanol, 1-cyclohexyl-3-methyl-3-nonanol,1-cyclohexyl-3,4-dimethyl-3-octanol,1-cyclohexyl-3,5-dimethyl-3-octanol,1-cyclohexyl-3,6-dimethyl-3-octanol,1-cyclohexyl-3,7-dimethyl-3-octanol,1-cyclohexyl-3,4,4-trimethyl-3-heptanol,1-cyclohexyl-3,5,5-trimethyl-3-heptanol,1-cyclohexyl-3,6,6-trimethyl-3-heptanol,1-cyclohexyl-5-ethyl-3-methyl-3-heptanol,1-cyclohexyl-3,5-dimethyl-3-heptanol,2,4-dicyclohexyl-2-methyl-2-butanol,1-cyclohexyl-4-cyclopentyl-3-methyl-3-pentanol,1-cyclohexyl-3-ethyl-3-hexanol, 1-cyclohexyl-3-ethyl-3-heptanol,1-cyclohexyl-3-ethyl-3-octanol and 1-cyclohexyl-3-ethyl-3-nonanol.

The present invention also provides compositions comprising a compoundof the formula (Ia)

and a compound of the formula (Ib)

where R¹ and R², independently of one another, are selected from groupsof the formula (C₃₋₇-cycloalkyl)_(x)-(C₁₋₇-alkyl)_(y), as defined above,and R¹ and R² together comprise in total 3 to 11 carbon atoms, inparticular 3 to 8 carbon atoms, preferably 3 to 5 carbon atoms andparticularly preferably 3 carbon atoms.

In these compositions, the weight ratio of the compound(s) of theformula (Ia) to the compound(s) of the formula (Ib) is in general in therange from 50:1 to 1000:1. Compositions of this kind can also comprisesmall amounts of a corresponding compound of the formula (IV)

and optionally of a corresponding compound of the formula (V)

which are formed by superreduction of the corresponding compounds of theformula (IIIa) or compounds of the formula (IIIb). The weight fractionof the total amount of the compound of the formula (IV) and optionallyof the compound of the formula (V) will generally not exceed 10% byweight, in particular 5% by weight, based on the corresponding compoundof the formula (Ia) and is, if present, in the range from 0.01 to 10% byweight, in particular in the range from 0.01 to 5% by weight, based onthe corresponding compound of the formula (Ia). It is of course alsopossible to separate off compounds of the formula (IV) and optionallypresent compounds of the formula (V), e.g. by a distillative route, suchthat the total amount of compound of the formula (IV) and optionallypresent compound of the formula (V) is less than 1% by weight, inparticular less than 0.5% by weight or less than 0.1% by weight, basedon the corresponding compound of the formula (Ia), A specificcomposition is concentrates, i.e. compositions which consistessentially, i.e., to at least 95% by weight, in particular at least 98%by weight and specifically at least 99% by weight or at least 99.5% byweight, of a compound of the formula (Ia) and small amounts ofcorresponding compound of the formula (Ib), e.g. compositions in whichthe weight ratio of the compound of the formula (Ia) to thecorresponding compound of the formula (Ib) is in the range from 50:1 to1000:1.

These concentrates can comprise corresponding compounds of the formula(IV) and and optionally corresponding compounds of the formula (V) inthe amounts specified above. Compositions in which the weight ratio ofthe compound of the formula (Ia) to the corresponding compound of theformula (Ib) is outside of the ranges specified here, can be prepared bymixing the compound of the formula (Ia) with the desired amount ofcompound of the formula (Ib). Compositions of this type are naturallylikewise provided by the present invention.

A compound of the formula (Ib) can be prepared from a correspondingcompound of the formula (IIIb) analogously to step b), i.e. by a processcomprising a heterogeneous-catalytic hydrogenation of the compound ofthe formula (IIIb). As regards the hydrogenation of the compound of theformula (IIIb), reference is made to the statements above relating tothe hydrogenation in step b) in their entirety.

Here, the procedure may involve firstly preparing a compound of theformula (IIIb) in a targeted manner and then subjecting it to aheterogeneous-catalytic hydrogenation analogously to step b) describedpreviously. A compound of the formula (IIIb) can be prepared in atargeted manner by reacting α-methylstyrene with a correspondingcompound of the formula (II) under the conditions specified above forstep a).

However, the procedure may also involve firstly preparing a compositionfrom a compound of the formula (IIIa) and a corresponding compound ofthe formula (IIIb), e.g. in the manner described above for step a),subjecting this composition to a heterogeneous-catalytic hydrogenationanalogously to step b) described previously, and separating theresulting composition, which comprises a corresponding compound of theformula (Ia) and a corresponding compound of the formula (Ib), into itsconstituents by distillation. The distillation can be carried outanalogously to customary fractional distillation processes. Suitabledevices for this are known to the person skilled in the art. Thenecessary conditions can be ascertained by routine experiments. As arule, the distillation takes place at reduced pressure.

In the compounds of the formulae (Ia) and (Ib) according to theinvention in which R¹ and R² are different, the chiral carbon atomcarrying the hydroxyl group can have a different configuration.Accordingly, the present invention also relates to the individualenantiomers and enantiomer mixtures, e.g. a racemate, of the compoundsof the formula (Ia) or of the formula (Ib) according to the invention.The enantiomers can be separated from one another with the help ofgenerally known processes, e.g. by means of crystallization, by means ofchiral column chromatography or by means of conversion to diastereomers,which are separated from one another by conventional chromatography anddistillation processes and are then converted again into the nowenantiomerically pure starting compounds. Moreover, the compounds of theformula (Ib) according to the invention can have a differentconfiguration at the chiral carbon atom carrying the cyclohexyl group.Accordingly, the present invention also relates to individualdiastereomers and diastereomer mixtures of the compounds of the formula(Ib) according to the invention. The diastereomers can be separated fromone another on account of their different physical properties byconventional processes, such as e.g. chromatography and distillationprocesses.

Compounds of the formulae (Ia) and (Ib) and the compositions andconcentrates likewise described here are odorous substances which can beused as fragrances or aroma substances and in particular in cosmeticcompositions, textile detergents and cleaners for hard surfaces.

The invention thus also relates to cosmetic compositions, textiledetergents and cleaners for hard surfaces comprising:

-   i. one or more compound(s) of the formula (Ia), in particular those    in which R¹ and R² together comprise in total 3 to 8 carbon atoms    and preferably 3 to 5 carbon atoms, particularly preferably    1-cyclohexyl-3-methyl-3-pentanol, or-   ii. a composition comprising a compound of the formula (Ia) and a    corresponding compound of the formula (Ib), in particular those in    which R¹ and R² comprise together in total 3 to 8 carbon atoms and    preferably 3 to 5 carbon atoms, particularly preferably where R¹ is    methyl and R² is ethyl.

Preferably, the compound(s) i. and composition ii., respectively, arecomprised as additives, i.e. said cosmetic compositions, textiledetergents and cleaners for hard surfaces, respectively, comprise, inaddition to i. or ii., compounds or compositions, which are suitable asuse as cosmetic compositions, textile detergents and cleaners for hardsurfaces.

Examples of suitable cosmetic compositions are in principle all cosmeticcompositions which usually comprise fragrances. These include, forexample, Eaux-de-Parfum, Eaux-de-Toilette, Eaux-de-Cologne, after shaveproducts such as lotions and creams, preshave products, perfumedfreshening wipes, hair removal creams and lotions, tanning creams andlotions, haircare compositions such as shampoos, hair rinses, hairsetting compositions, hair gels, hair tinting compositions, hair waxes,hairsprays, setting foams, hair mousses, end fluids, neutralizers forpermanent waves, hair colorants and bleaches or “hot-oil treatments”,also skin cleansers such as soaps, washing gels, shower gels, bodycarecompositions such as creams, oils, lotions and the like for the skin,such as e.g. products for caring for the hands, the face or the feet,sunscreens, deodorants and antiperspirants, Skin disinfectants, insectrepellents, and also decorative cosmetic products. Depending on thefield of use, the cosmetic compositions can be formulated as aqueous oralcoholic liquid, oil, (aerosol) spray, (aerosol) foam, mousse, gel, gelspray, cream, lotion, powder, tabs or wax.

Detergents and cleaners include compositions for the cleaning and/ordisinfection of surfaces, such as, for example, household cleaners,neutral cleaners, toilet cleaners, floor cleaners, carpet cleaners,window cleaners, polishes, furniture care products, liquid and soliddishwashing detergents, liquid and solid machine dishwashing detergents,also compositions for the cleaning or treatment of textiles such assolid, semisolid or liquid textile detergents, laundry after-treatmentcompositions, fabric softeners, ironing aids, textile fresheners, fabricpreconditioners, washing soaps, washing tablets and the like.

Furthermore, the compounds and compositions according to the inventioncan be used as fragrance constituent in other fragrance-containingproducts such as air purifiers, lamp oils, candles, room air improvers,toilet blocks and the like.

The compound of the formula (Ia) in the compositions according to theinvention, cosmetic compositions, textile detergents, cleaners and usescan for example be selected from 1-cyclohexyl-3-methyl-3-pentanol,1-cyclohexyl-3-methyl-3-hexanol, 1-cyclohexyl-3-methyl-3-heptanol,1-cyclohexyl-3-methyl-3-octanol, 1-cyclohexyl-3-methyl-3-nonanol,1-cyclohexyl-3,4-dimethyl-3-octanol, 1-cyclohexyl-3,5-dimethyl-3′octanol, 1-cyclohexyl-3,6-dimethyl-3-octanol,1-cyclohexyl-3,7-dimethyl-3-octanol,1-cyclohexyl-3,4,4-trimethyl-3-heptanol,1-cyclohexyl-3,5,5-trimethyl-3-heptanol,1-cyclohexyl-3,6,6-trimethyl-3-heptanol,1-cyclohexyl-5-ethyl-3-methyl-3-heptanol,1-cyclohexyl-3,5-dimethyl-3-heptanol,2,4-Dicyclohexyl-2-methyl-2-butanol,1-cyclohexyl-4-cyclopentyl-3-methyl-3-pentanol,1-cyclohexyl-3-ethyl-3-hexanol, 1-cyclohexyl-3-ethyl-3-heptanol,1-cyclohexyl-3-ethyl-3-octanol and 1-cyclohexyl-3-ethyl-3-nonanol.

The invention is illustrated in more detail by reference to thefollowing examples:

Example 1 Preparation of the Hydrogenated Catalyst

The support material used was a spherical SiO₂ support (type AF125 fromBASF SE) with a sphere diameter of 3 to 5 mm and a bulk density of 0.49kg/l. The BET surface area was 337 m2/g, the water absorption (WA) was0.83 ml/g. For the impregnation, a 14.25% by weight ruthenium(III)acetate solution in acetic acid (from Umicore) was used.

200 g of support were introduced as initial charge into a round-bottomedflask. 15 g of the ruthenium acetate solution were diluted to 150 mlwith distilled water (90% WA). The support material was introduced asinitial charge into the distillation column of a rotary evaporator andthe first quarter of the solution was pumped onto the support materialwith a slight vacuum at 3 to 6 rpm. When the addition was complete, thesupport was left in the rotary evaporator for a further 10 minutes at 3to 6 rpm in order to homogenize the catalyst. Thisimpregnation/homogenization step was repeated three times until all ofthe solution had been applied to the support. The support materialtreated in this way was dried under agitation in the rotary dryer at140° C., then reduced for 3 h at 200° C. in a stream of hydrogen (20 l/hH₂; 10 l/h N₂) and passivated at 25° C. (5% air in N₂, 2 h). Theresulting catalyst A according to the invention comprised 0.34% byweight of ruthenium, based on the total weight of the catalyst.

Step A Example 2 Preparation of 3-Methyl-1-Phenyl-3-Pentanol

The reaction of styrene and 2-butanol was carried out in a continuouslyoperated laboratory plant. This comprised a 300 ml autoclave which wasoperated with pressure regulation. Thus, the amount removed correspondedat all times to the amount introduced. The removed reaction mixture wascooled, decompressed and collected in a discharge container.

A solution of styrene in 2-butanol (20% by weight, 100 g/h) was pumpedcontinuously at an average temperature of 390° C. in the reactor throughthe laboratory plant. The conversion of styrene was 84.0% and, in thesteady state, 14.7 g/h of 3-methyl-1-phenyl-3-pentanol were obtained.

Step B Example 3 Preparation of 1-Cyclohexyl-3-Methyl-3-Pentanol

A 300 ml autoclave was initially charged with 5.6 g of3-methyl-1-phenyl-3-pentanol, dissolved in 94.4 g of tetrahydrofuran,and 1.6 g of a catalyst prepared according to Example 1 (0.35% rutheniumon silicon dioxide). The autoclave was flushed three times with nitrogenand then hydrogenated for 10 hours at 160° C. and a hydrogen pressure of160 bar. The product was analyzed by gas chromatography(polydimethylsiloxane DB1, 30 m, internal diameter: 0.25 mm, filmthickness: 0.25 μm, 50° C., 5 min isotherm, −6° C./min, 290° C., 219 minisotherm). The conversion was 99.9%, the selectivity 93%.

The invention claimed is:
 1. A method for improving the olfactoryproperties and/or concealing undesired intrinsic odors of a cosmeticcomposition, textile detergent or cleaner for hard surfaces, the methodcomprising adding a compound of formula (Ia) to the cosmeticcomposition, the textile detergent or the cleaner for hard surfaces,

wherein R₁ and R₂, independently of one another, are selected fromC₄₋₇-cycloalkylalkyl- with a total of 4 to 7 carbon atoms,C₃₋₇-cycloalkyl-, which is optionally substituted with 1, 2, or 3C₁₋₇-alkyl, and C₁₋₇-alkyl-, and R₁ and R₂ together comprise in total 3to 11 carbon atoms.
 2. The method according to claim 1, wherein R¹ andR², independently of one another, are selected from C₁₋₇-alkyl-.
 3. Themethod according to claim 1, wherein R¹ is methyl and R² is ethyl. 4.The method according to claim 1, wherein R¹ and R² together comprise intotal 3 to 5 carbon atoms.
 5. The method according to claim 1, whereinthe adding of the compound of formula (Ia) includes adding a compound offormula (Ib)


6. The method according to claim 1, wherein R¹ and R², independently ofone another, are selected from C₁₋₇-alkyl, and C₄₋₇-cycloalkylalkyl-with a total of 4 to 7 carbon atoms.
 7. The method according to claim 1,wherein R¹ and R², independently of one another, are selected fromC₁₋₇-alkyl, and C₃₋₇-cycloalkyl-, which is optionally substituted with1, 2, or 3 C₁₋₇-alkyl.
 8. The method according to claim 2, wherein thecompound of formula (1a) is selected from the from consisting of1-cyclohexyl-3-methyl-3-hexanol, 1-cyclohexyl-3-methyl-3-heptanol,1-cyclohexyl-3-methyl-3-octanol, 1-cyclohexyl-3-methyl-3-nonanol,1-cyclohexyl-3,4-dimethyl-3-octanol,1-cyclohexyl-3,5-dimethyl-3-octanol,1-cyclohexyl-3,6-dimethyl-3-octanol,1-cyclohexyl-3,7-dimethyl-3-octanol,1-cyclohexyl-3,4,4-trimethyl-3-heptanol,1-cyclohexyl-3,5,5-trimethyl-3-heptanol,1-cyclohexyl-3,6,6-trimethyl-3-heptanol,1-cyclohexyl-5-ethyl-3-methyl-3-heptanol,1-cyclohexyl-3,5-dimethyl-3-heptanol,2,4-dicyclohexyl-2-methyl-2-butanol,1-cyclohexyl-4-cyclopentyl-3-methyl-3-pentanol,1-cyclohexyl-3-ethyl-3-hexanol, 1-cyclohexyl-3-ethyl-3-heptanol,1-cyclohexyl-3-ethyl-3-octanol, and 1-cyclohexyl-3-ethyl-3-nonanol.